CN110121386A - The method for producing pure air-flow - Google Patents
The method for producing pure air-flow Download PDFInfo
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- CN110121386A CN110121386A CN201780065693.4A CN201780065693A CN110121386A CN 110121386 A CN110121386 A CN 110121386A CN 201780065693 A CN201780065693 A CN 201780065693A CN 110121386 A CN110121386 A CN 110121386A
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- Prior art keywords
- absorbing medium
- flow
- hydrogen sulfide
- air
- carbon dioxide
- Prior art date
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- 238000004519 manufacturing process Methods 0.000 title description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 70
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 41
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 39
- 238000000034 method Methods 0.000 claims abstract description 38
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 35
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 26
- 239000007789 gas Substances 0.000 claims abstract description 16
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 13
- 150000001412 amines Chemical class 0.000 claims abstract description 12
- 239000011593 sulfur Substances 0.000 claims abstract description 12
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 12
- 239000002904 solvent Substances 0.000 claims description 10
- 150000003839 salts Chemical class 0.000 claims description 4
- FAGUFWYHJQFNRV-UHFFFAOYSA-N tetraethylenepentamine Chemical compound NCCNCCNCCNCCN FAGUFWYHJQFNRV-UHFFFAOYSA-N 0.000 claims description 4
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 2
- RPNUMPOLZDHAAY-UHFFFAOYSA-N Diethylenetriamine Chemical class NCCNCCN RPNUMPOLZDHAAY-UHFFFAOYSA-N 0.000 claims description 2
- 238000002425 crystallisation Methods 0.000 claims description 2
- 230000008025 crystallization Effects 0.000 claims description 2
- 238000000909 electrodialysis Methods 0.000 claims description 2
- 239000011552 falling film Substances 0.000 claims description 2
- 239000003456 ion exchange resin Substances 0.000 claims description 2
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- VILCJCGEZXAXTO-UHFFFAOYSA-N 2,2,2-tetramine Chemical compound NCCNCCNCCN VILCJCGEZXAXTO-UHFFFAOYSA-N 0.000 claims 2
- WGIAYBNWTYECJD-UHFFFAOYSA-N 1-ethoxypiperazine Chemical compound CCON1CCNCC1 WGIAYBNWTYECJD-UHFFFAOYSA-N 0.000 claims 1
- 229960001124 trientine Drugs 0.000 claims 1
- 229920000768 polyamine Polymers 0.000 abstract description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 8
- 230000004913 activation Effects 0.000 abstract description 5
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 4
- 150000003335 secondary amines Chemical group 0.000 abstract description 4
- 238000001179 sorption measurement Methods 0.000 abstract description 4
- 125000001302 tertiary amino group Chemical group 0.000 abstract 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 abstract 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 abstract 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 abstract 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 8
- 230000009102 absorption Effects 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 6
- 150000003512 tertiary amines Chemical group 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 150000003141 primary amines Chemical group 0.000 description 3
- 238000004073 vulcanization Methods 0.000 description 3
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- AGGKEGLBGGJEBZ-UHFFFAOYSA-N tetramethylenedisulfotetramine Chemical compound C1N(S2(=O)=O)CN3S(=O)(=O)N1CN2C3 AGGKEGLBGGJEBZ-UHFFFAOYSA-N 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 125000001301 ethoxy group Chemical group [H]C([H])([H])C([H])([H])O* 0.000 description 1
- 239000002343 natural gas well Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8612—Hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/2041—Diamines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20415—Tri- or polyamines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20436—Cyclic amines
- B01D2252/20447—Cyclic amines containing a piperazine-ring
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/50—Combinations of absorbents
- B01D2252/504—Mixtures of two or more absorbents
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The method that the present invention relates to a kind of to remove hydrogen sulfide and carbon dioxide from feed stream.The H2S in feed stream is set to be converted into elementary sulfur in Claus unit (Claus unit).Contact at least part of gained air-flow under the pressure in uptake zone, between 0.9 and 2 bars with aqueous poor absorbing medium.Aqueous poor absorbing medium used includes one or more amine, and the amine is selected from :-lacking the polyamines with the tertiary amine functional group for being enough to neutralize carbamic pKa, at least one primary amine functional group of the polyamines has the pKa at 25 DEG C less than 10.0；Lack the polyamines with the tertiary amine functional group for being enough to neutralize carbamic pKa, at least one secondary amine functional groups of the polyamines have the pKa at 25 DEG C for each adsorption of nitrogen less than 10.0.The method is compared to being related to being improved with the method that (activation) MDEA carries out Crouse's exhaust-gas treatment.While realizing that CO2 is effectively removed, the less simple flow of equipment can be used.
Description
Technical field
The present invention relates to a kind of methods for removing hydrogen sulfide and carbon dioxide from feed stream.
Background technique
Air-flow from the natural gas well is typically " sour gas " stream, because they generally comprise carbon dioxide and vulcanization
Hydrogen.Before such air-flow can further use, need to remove H2S and CO2.
Method from removal H2S and CO2 in " sour gas " is well known in the art.Such method is typically comprised from gas
The absorption step of sulfur-containing compound and carbon dioxide is removed in state feeding flow, this is by making such gaseous feed stream and solvent
(such as amine solvent) contacts to realize in absorption tower.To be commonly referred to as that the pure air-flow of " sweet gas body " and load have
The solvent of pollutant.The solvent of load typically regenerates in stripper, obtain lean solvent and H2S comprising rather high concentration and
The air-flow of CO2.Lean solvent can be recycled in absorption tower.
It can be in the air-flow of H2S and CO2 of the second absorption stage processing comprising rather high concentration.For example, can to its into
Row Claus method (Claus process) and generate elementary sulfur and Crouse's exhaust gas.Crouse's exhaust gas be commonly subjected to H2S and/or
CO2 removes program.
Gone from Crouse's exhaust gas removing carbon dioxide common method be with methyl diethanolamine (MDEA) or with activate
MDEA is handled under high pressure.However, MDEA is sensitive to degradation in the presence of H2S.Therefore, logical before being handled with (activation) MDEA
Often removal H2S.(activation) MDEA processing is generally conducted at an elevated pressure.Due to Crouse's exhaust gas (also after H2S removal) usually place
Under atmospheric pressure, therefore this needs to pressurize to Crouse's exhaust gas before (activation) MDEA processing.In addition, since the technique is
It carries out under high pressure, therefore the size of absorptive unit is restricted.Therefore it is needed when disposing extensive Crouse's waste gas stream more
A compressor and multiple absorptive units.
It is an object of the present invention to a kind of improved methods for removing hydrogen sulfide and carbon dioxide from feed stream, especially
It is when it is related to claus tail-gas clean-up.One target is to realize effective CO2 removal.Another target is simple flow,
It is preferred that reducing required equipment.Another target is to reduce the energy consumption in technique.At the same time, it is desirable to which processing method deposits H2S
Less sensitive.
Summary of the invention
The present invention relates to it is a kind of for from feed stream remove hydrogen sulfide and carbon dioxide method, the method includes
Following steps:
(i) hydrogen sulfide in feed stream is made to be converted to elementary sulfur in Claus unit, thus obtain elementary sulfur and
The air-flow of hydrogen sulfide and carbon dioxide comprising content reduction；
(ii) at least part of air-flow obtained by step (i) is contacted in uptake zone to absorb with aqueous poor absorbing medium
Carbon dioxide obtains the processing air-flow and useless absorbing medium of poor carbon dioxide；
Wherein the pressure in uptake zone used in step (ii) is between 0.9 and 2 bar, the range preferably between 0.9 and 1.5 bar
It is interior；And
Wherein aqueous poor absorbing medium used in step (ii) includes one or more amine, and the amine is selected from:
Lack the polyamines with a effective amount of tertiary amine functional group for being enough to neutralize carbamic pKa, the polyamines is extremely
A few primary amine functional group has the pKa at 25 DEG C less than 10.0,
Lack the polyamines with a effective amount of tertiary amine functional group for being enough to neutralize carbamic pKa, the polyamines is extremely
Few secondary amine functional groups have the pKa at 25 DEG C for each adsorption of nitrogen less than 10.0.
Compared to the method for being related to carrying out Crouse's exhaust-gas treatment with (activation) MDEA, the present invention is a kind of improved side
Method.
Effective CO2 removal is realized according to the method for the present invention, while simple flow can be used.Due to not needing pair
The pressurization of Crouse's exhaust gas, therefore the method can be carried out with less equipment.This is but also energy consumption reduces.In addition, above-listed amine
The processing method of class is less sensitive to H2S existing for Claus unit downstream.
Specific embodiment
The present invention relates to a kind of for removing the side of hydrogen sulfide and carbon dioxide from feed stream according to claim 1
Method.Feed stream includes hydrogen sulfide and includes carbon dioxide and optionally include other pollutants, such as COS.
In step (i), the hydrogen sulfide in feed stream is made to be converted into elementary sulfur in Claus unit.Acquisition contains
Measure the air-flow of reduced hydrogen sulfide.Claus method cannot or can hardly remove removing carbon dioxide, and therefore carbon dioxide is still deposited
It is in air-flow.
Preferably, feed stream used in step (i) includes the at most carbon dioxide of 25vol%.
There are two steps for the preferred tool of step (i).In step (ia), the hydrogen sulfide in feed stream is in Claus unit
It is converted into elementary sulfur, to obtain elementary sulfur and hydrogen sulfide and the carbonated air-flow of packet comprising content reduction.In step
Suddenly in (ib), even more hydrogen sulfide is removed from air-flow obtained by (ia) by means of solvent.
In step (ib), made a return journey vulcanisation hydrogen using amine-containing solvent is wrapped, preferably selectively remove hydrogen sulfide without
Removing carbon dioxide is hardly removed in removal.It obtains the hydrogen sulfide being further reduced comprising content and still also includes the logistics of CO2.
In step (ib), hydrogen sulfide is removed preferably by means of shell Crouse exhaust-gas treatment (SCOT) method.In step (ib)
Another appropriate method of vulcanisation hydrogen is using solvent, such as Flexsorb (ExxonMobil).
In step (ii), make at least part of air-flow obtained by step (i) with aqueous poor absorbing medium in uptake zone
Contact.Carbon dioxide is absorbed.Obtain the processing air-flow of poor carbon dioxide.Obtain useless absorbing medium.
Pressure in uptake zone used in step (ii) is the range between 0.9 and 2 bar, preferably between 0.9 and 1.5 bar
It is interior.
Aqueous poor absorbing medium used in step (ii) includes one or more amine, and the amine is selected from:
Lack the polyamines with a effective amount of tertiary amine functional group for being enough to neutralize carbamic pKa, the polyamines is extremely
A few primary amine functional group has the pKa at 25 DEG C less than 10.0,
Lack the polyamines with a effective amount of tertiary amine functional group for being enough to neutralize carbamic pKa, the polyamines is extremely
Few secondary amine functional groups have the pKa at 25 DEG C for each adsorption of nitrogen less than 10.0.
" lack the polyamines with a effective amount of tertiary amine functional group for being enough to neutralize carbamic pKa, the polyamines extremely
It is diethylenetriamines (DETA), Sanya that a few primary amine functional group, which has the preferred embodiment of the pKa " at 25 DEG C less than 10.0,
Tetramine (TETA), tetren (TEPA) and its mixture.
" lack the polyamines with a effective amount of tertiary amine functional group for being enough to neutralize carbamic pKa, the polyamines extremely
It is N- (2- that few secondary amine functional groups, which have the preferred embodiment of the pKa " at 25 DEG C for each adsorption of nitrogen less than 10.0,
Ethoxy) piperazine.
Since step (ii) does not need to carry out under high pressure, exist freely in terms of the design and size of absorptive unit
Degree.When disposing extensive Crouse's waste gas stream, in most cases, do not need single using multiple compressors and multiple absorptions
Member.On the contrary, in most cases, avoiding being sufficient between step (i) and step (ii) using compressor.It in addition or can
Alternatively, in most cases, it is sufficient using single absorptive unit.Therefore, in most cases, simple single
Sequence is sufficient.
Preferably, the air-flow contacted in uptake zone with aqueous poor absorbing medium in step (ii), in step (i) and step
(ii) 2 bars or more are not pressurized between.Preferably, the gas contacted in uptake zone with aqueous poor absorbing medium in step (ii)
Stream between step (i) and step (ii), is within the compressor not pressurized.Due to needing air-flow, the pressure of air-flow can be omited
Higher than atmospheric pressure.The pressure of air-flow used in step (ii) is the model between 0.9 and 2 bar, preferably between 0.9 and 1.5 bar
In enclosing.
Preferably, step (i) is resulting at least 70%, preferably at least 85%, more preferably at least 95%, more preferable entire gas
Stream in step (ii), it is processed in single absorptive unit.
Method of the invention is less sensitive to H2S or other sulphur components.Therefore, poor in uptake zone in step (ii)
Absorbing medium may include hydrogen sulfide and be optionally present COS.
Therefore, the H2S for the content reduction being still in air-flow to be processed in step (ii) is without being removed.Cause
This, for example, the resulting gas of step (i) is before step (ii) without burning.Preferably, in step (ii) in uptake zone with
The air-flow of aqueous poor absorbing medium contact, is not burned between step (i) and step (ii).This saves complexity and equipment.
Preferably, the air-flow contacted in uptake zone with aqueous poor absorbing medium in step (ii) includes hydrogen sulfide, dioxy
The COS for changing carbon and being optionally present.
In a preferred embodiment, the method comprises the steps of: after step (ii)
(iii) it regenerates the resulting useless absorbing medium of step (ii) in renewing zone, generates regenerated aqueous absorption and be situated between
Matter and carbon dioxide；With
(iv) at least part of step (iii) regenerated aqueous absorbing medium obtained is recycled to step (ii).
In a preferred embodiment, a part of the resulting regenerated aqueous absorbing medium of step (iii) is made to be recycled to step
Suddenly (ii) and the method comprise the steps of: after step (iv)
(v) heat stable salt is removed from the second part of the resulting regenerated aqueous absorbing medium of step (iii), preferably by
In ion exchange resin, electrodialysis, crystallization or recuperation of heat；With
At least part of the gained regenerated aqueous absorbing medium for the heat stable salt content reduction that (VI) obtains step (v)
It is recycled to step (ii).
Preferably, step (iii) is carried out in reboiler,
It is preferred that in kettle type reboiler, forced circulating reboiler, burning reboiler, falling-film reboiler, direct steam reboiler
Or in thermosyphon, carried out preferably in thermosyphon.
Claims (9)
1. a kind of method for removing hydrogen sulfide and carbon dioxide from feed stream, the method comprise the steps of:
(i) hydrogen sulfide in the feed gas stream is made to be converted to elementary sulfur in Claus unit, thus obtain elementary sulfur and
Hydrogen sulfide comprising content reduction and the carbonated air-flow of packet；
(ii) at least part of the resulting air-flow of step (i) is contacted in uptake zone with aqueous poor absorbing medium, with
Absorbing carbon dioxide obtains the processing air-flow and useless absorbing medium of poor carbon dioxide；
The pressure in the uptake zone that wherein step (ii) uses is between 0.9 and 2 bar, preferably between 0.9 and 1.5 bar
In range；And
The aqueous poor absorbing medium that wherein step (ii) uses includes one or more amine, and the amine is selected from:
Diethylenetriamines (DETA), trien (TETA), tetren (TEPA) and its mixture,
N- (2- ethoxy) piperazine.
2. according to the method described in claim 1, wherein the resulting air-flow of step (i) at least 70%, preferably at least
85%, more preferably at least 95% in step (ii), it is processed in single absorptive unit.
3. method according to claim 1 or 2 wherein contacts in uptake zone in step (ii) with aqueous poor absorbing medium
The air-flow do not burned between step (i) and step (ii).
4. method according to any one of the preceding claims is wherein absorbing in step (ii) with aqueous poor absorbing medium
The air-flow contacted in area includes hydrogen sulfide, carbon dioxide and the COS being optionally present.
5. method according to any one of the preceding claims, wherein step (i) includes:
(ia) elementary sulfur is converted in Claus unit by the hydrogen sulfide in the feed stream, thus obtain elementary sulfur and
The air-flow of hydrogen sulfide and carbon dioxide comprising content reduction；
(ib) even more hydrogen sulfide is removed from (ia) resulting described air-flow by means of wrapping amine-containing solvent, to obtain
Logistics comprising the hydrogen sulfide that content is further reduced.
6. method according to any one of the preceding claims, the method has following additional step:
(iii) regenerate the resulting useless absorbing medium of step (ii) in renewing zone, with generate regenerated aqueous absorbing medium and
Carbon dioxide；With
(iv) at least part of step (iii) described regenerated aqueous absorbing medium obtained is recycled to step (ii).
7. according to the method described in claim 6, making the resulting regenerated aqueous of step (iii) wherein in step (iv)
A part of absorbing medium, which is recycled to step (ii) and the method, has following additional step:
Heat stable salt is removed from the second part of the resulting regenerated aqueous absorbing medium of step (iii), preferably by means of
Ion exchange resin, electrodialysis, crystallization or recuperation of heat carry out；With
(vi) make at least one as obtained by step (v) with the gained regenerated aqueous absorbing medium of reduced heat stable salt content
Divide and is recycled to step (ii).
8. method according to claim 6 or 7, wherein step (iii) is carried out in reboiler,
It is preferred that in kettle type reboiler, forced circulating reboiler, burning reboiler, falling-film reboiler, direct steam reboiler or heat
In siphon device, carried out preferably in thermosyphon.
9. method according to any one of the preceding claims, wherein the feed stream used in step (i) includes
The at most carbon dioxide of 25vol%.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP16196691 | 2016-11-01 | ||
| EP16196691.6 | 2016-11-01 | ||
| PCT/EP2017/077852 WO2018083076A1 (en) | 2016-11-01 | 2017-10-31 | Process for producing a purified gas stream |
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| CN110121386A true CN110121386A (en) | 2019-08-13 |
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| CN201780065693.4A Pending CN110121386A (en) | 2016-11-01 | 2017-10-31 | The method for producing pure air-flow |
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| US (1) | US10888816B2 (en) |
| CN (1) | CN110121386A (en) |
| BR (1) | BR112019008894B1 (en) |
| CA (1) | CA3041192A1 (en) |
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| CN112794327B (en) * | 2020-12-31 | 2022-05-24 | 中国科学院山西煤炭化学研究所 | Method and device for preparing carbonyl sulfide from carbon dioxide and hydrogen sulfide mixed gas |
| US11407667B1 (en) | 2021-06-06 | 2022-08-09 | Christopher R. Moylan | Systems and methods for removal of carbon dioxide from seawater |
| US11685673B2 (en) | 2021-06-06 | 2023-06-27 | Christopher R. Moylan | Systems and methods for removal of carbon dioxide from seawater |
| CN115990394B (en) * | 2023-03-24 | 2023-06-02 | 成都益志科技有限责任公司 | Desalination and sodium removal system and method in ionic liquid desulfurization |
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| RU2748547C2 (en) | 2021-05-26 |
| US20200047117A1 (en) | 2020-02-13 |
| WO2018083076A1 (en) | 2018-05-11 |
| BR112019008894B1 (en) | 2023-10-03 |
| RU2019116687A3 (en) | 2020-11-30 |
| BR112019008894A2 (en) | 2019-08-13 |
| US10888816B2 (en) | 2021-01-12 |
| CA3041192A1 (en) | 2018-05-11 |
| RU2019116687A (en) | 2020-11-30 |
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